CN210656586U - Wastewater treatment device based on combination of MBR and ozone multi-point addition - Google Patents
Wastewater treatment device based on combination of MBR and ozone multi-point addition Download PDFInfo
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- CN210656586U CN210656586U CN201921371114.1U CN201921371114U CN210656586U CN 210656586 U CN210656586 U CN 210656586U CN 201921371114 U CN201921371114 U CN 201921371114U CN 210656586 U CN210656586 U CN 210656586U
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 161
- 238000004065 wastewater treatment Methods 0.000 title claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 177
- 239000012528 membrane Substances 0.000 claims abstract description 116
- 230000003197 catalytic effect Effects 0.000 claims abstract description 78
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 72
- 238000000034 method Methods 0.000 claims description 28
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- 238000007254 oxidation reaction Methods 0.000 claims description 12
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
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- 239000000126 substance Substances 0.000 abstract description 18
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- 230000009471 action Effects 0.000 abstract description 7
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract 1
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Abstract
The application discloses effluent treatment plant based on MBR and ozone multiple spot are thrown and combine. This effluent treatment plant includes: the device comprises a membrane bioreactor, a suction pump, a membrane effluent lifting pool, a membrane effluent lifting pump, a catalytic reactor and a discharge water pool; the water treated by the membrane bioreactor is directly connected with a water outlet suction pump through a membrane water collecting pipe, is led to a membrane water outlet lifting pool through the suction pump, is lifted to the inlet end of the catalytic reactor through the pump, and is discharged to a water discharging pool after being treated by the catalytic reactor. The catalytic reactor is a pipeline type mixing reactor, a hydrogen peroxide dosing device is arranged at the water inlet end of the catalytic reactor, a mixing area is arranged in the catalytic reactor, and the catalytic reactor is used for fully mixing and reacting ozone and hydrogen peroxide, wherein the ozone is in a double-layer structureHydroxyl free radicals are generated under the action of oxygen water, so that macromolecular organic matters which are difficult to degrade in water are oxidized and degraded into micromolecular substances and CO2And water is mixed, and the water after reaction in the reaction zone is discharged to a discharge water pool through a water outlet.
Description
Technical Field
The utility model relates to a waste water treatment field, concretely relates to waste water treatment device based on Membrane Bioreactor (MBR) throws with ozone multiple spot and throws combination.
Background
Coal chemical industry enterprises are water consumers, and aiming at the shortage of water resources and the increasing environmental protection requirement, the coal chemical industry enterprises can treat the wastewater generated from the source, and the treated wastewater adopts a double-membrane method to recover the part of water resources. However, due to the characteristic of difficult biochemical and thorough degradation in the coal chemical wastewater, the conventional biochemical process cannot meet the requirement that the effluent directly enters a reuse water system, and the conventional sewage treatment process has technical bottlenecks and technical risks. The wastewater which does not reach the standard enters a subsequent reuse water system to cause organic pollution and the pollution and blockage of suspended solid and colloid.
Organic pollutants dissolved in wastewater are the most difficult problems to solve by the existing reverse osmosis membrane, ultrafiltration can only intercept a small amount of macromolecular organic matters or non-soluble organic matters with the pore diameter larger than that of the ultrafiltration membrane, and most of organic matters with smaller molecular weight pass through the ultrafiltration membrane to cause fouling and blockage of the reverse osmosis membrane, so that the performance of the reverse osmosis membrane is seriously degraded, for example, the desalination rate and the water yield of the reverse osmosis membrane are rapidly and greatly reduced. And the pollution of suspended solids and colloid seriously influences the reverse osmosis and the operation performance of a nanofiltration membrane element, and mainly shows that the produced water flow is reduced, the differential pressure of a membrane system is increased, and the desalination rate of the membrane is influenced. Therefore, the reasonable selection of the process to more effectively reduce COD, suspended matters and colloid of the effluent of the biochemical system becomes the first difficult problem of the coal chemical industry refractory wastewater project.
The biodegradability of the refractory wastewater in the coal chemical industry is poor, for example, after the traditional biochemical treatment such as an anoxic/aerobic method (A/O) and a Sequencing Batch Reactor (SBR) is adopted, COD cannot be effectively degraded by further adopting a biomembrane method such as biological contact oxidation and an aeration biological filter method, suspended matters and turbidity of effluent do not meet the requirements, the water quality entering a reuse water treatment system can be ensured only by arranging a high-efficiency clarification tank, a mechanical filtration process and an advanced oxidation process, and the process is long, high in operation cost and high in maintenance and management cost.
Common advanced oxidation technologies include ozone advanced oxidation, Fenton improvement method and the like, and the technology has the advantages of wide application range, mature technology, stability and reliability. The standard-reaching discharge process of the coal chemical industry refractory wastewater which is widely applied usually needs to ensure that the concentration of organic matters in the wastewater reaches the standard by means of ozone advanced oxidation, and in the traditional ozone contact process, the ozone utilization rate is low, the energy consumption is high, the treatment effect is unstable, and a concrete reaction tank with a large occupied area needs to be arranged, so that the water outlet effect is poor. In addition, the effluent of the traditional biochemical process directly enters an advanced oxidation system without pretreatment, so that serious pollution and blockage are generated. In addition, the Fenton improved process causes large amount of chemical sludge, high chemical agent adding cost, more matched structures and equipment, increases the content of soluble solids in the wastewater, and is uneconomical and unsuitable.
SUMMERY OF THE UTILITY MODEL
In view of this, to the problems that the existing treatment device has, the application provides a wastewater treatment device based on the combination of a membrane bioreactor and ozone multipoint adding, and the treatment method of the treatment device is simple, and the treatment device is used for improving the treatment efficiency of coal chemical industry refractory wastewater, and has the advantages of good water outlet effect, simple process flow, low operation cost and high automation degree.
In order to achieve the above-mentioned purpose, the present application adopts the following scheme,
a wastewater treatment device based on combination of MBR and ozone multi-point feeding is characterized by comprising a membrane bioreactor, a suction pump, a catalytic reactor and a discharge water tank,
the membrane bioreactor is provided with a water outlet which is arranged at the upper part of the membrane component and is connected with one end of a membrane water collecting pipe, the other end of the membrane water collecting pipe is connected with a suction pump,
the catalytic reactor has the water inlet, and it is connected to the suction pump through the pipeline, and the delivery port, it is connected to the emission pond through the pipeline, and port is thrown to a plurality of ozone, and it is used for to catalytic reactor's intraductal injection ozone, hydrogen peroxide solution throw the port, and it is located near the water inlet, be used for to catalytic reactor's intraductal injection hydrogen peroxide solution, wherein, the water process of membrane bioreactor processing is taken out and is introduced catalytic reactor, and the water after ozone catalytic oxidation handles is discharged to the emission pond through its export in catalytic reactor.
Preferably, the dosage of the ozone at each ozone dosage port is 20 mg/L-80 mg/L.
Preferably, the wastewater treatment device also comprises a membrane effluent lifting pool, and the water treated by the membrane bioreactor is introduced to the membrane effluent lifting pool through a suction pump;
the membrane water outlet lifting pump is provided with a first water inlet end which is connected into the membrane water outlet lifting pool through a pipeline, and a first water outlet end which is connected to a water inlet of the catalytic reactor through a pipeline and is used for lifting water in the membrane water outlet lifting pool to the catalytic reactor.
Preferably, the total ozone dosage of the plurality of ozone dosage ports is between 0 and 240 mg/L.
Preferably, the adding amount and adding mass ratio of the ozone to the hydrogen peroxide is 2-3: 1.
preferably, the adding mass ratio of the ozone to the hydrogen peroxide is 2.83: 1.
preferably, the ozone adding pressure is 0.09 MPa.
Preferably, the catalytic reactor adopts a pipeline type mixing reactor, and comprises a water inlet, a water outlet, a first ozone adding port, a second ozone adding port and a third ozone adding port, wherein the first ozone adding port, the second ozone adding port and the third ozone adding port are respectively connected to an ozone generator through pipelines, a hydrogen peroxide adding port is configured near the water inlet, water flows to the catalytic reactor through the water inlet during the operation of the catalytic reactor, and the hydrogen peroxide adding port injects the hydrogen peroxide into the water, and the first ozone adding port, the second ozone adding port and the third ozone adding port inject the ozone into the water in the pipeline.
Preferably, the distance L1 for water to flow through between the first ozone adding port and the second ozone adding port is equal to the distance L2 for water to flow through between the second ozone adding port and the third ozone adding port.
Preferably, the ratio of the flowing distance L3 between the third ozone adding port and the water inlet to the flowing distance L between the water inlet and the water outlet is 0.3-0.7.
The embodiment of the application also provides a wastewater treatment method based on combination of MBR and ozone multipoint feeding, which is characterized by comprising the wastewater treatment device of any one of claims 1-8, and the method comprises the following steps:
s1, water to be treated flows into a membrane bioreactor;
s2, separating water from activated sludge in the membrane bioreactor based on the membrane bioreactor water;
s3, lifting the separated water to a catalytic reactor, feeding hydrogen peroxide into the pipe through a hydrogen peroxide feeding end on the water inlet side of the catalytic reactor while feeding water, and feeding ozone into the pipe at a plurality of ozone feeding points;
and S4, discharging the water treated by the catalytic reactor into a discharge water tank.
Preferably, the flow rate of water in the pipeline of the catalytic reactor in the S3 is 1-3 m/S, and the ozone dosage at each dosage point is 20-80 mg/L.
Advantageous effects
Compared with the prior art, the embodiment of the application has the following advantages:
1) by utilizing the conditions of low COD concentration, low suspended matter concentration and low turbidity of the membrane bioreactor effluent, the membrane module effluent directly enters the catalytic reactor, the processes of a sedimentation tank, filtration and the like are omitted, the floor area is saved, the volume of a civil engineering tank is saved, the process flow is simple, the automation degree is high, and the operation cost and the investment are reduced.
2) The catalytic reactor in the form of a pipeline can be flexibly designed according to requirements, is convenient to install and occupies a smaller area. In the reaction process, the contact of ozone, wastewater and hydrogen peroxide is more accurate and sufficient, hydroxyl free radicals are more favorably generated, the oxidizing capability is strong, and meanwhile, the reactor is simple to maintain and has long service life.
Drawings
Other features and aspects of the present invention will become apparent from the following detailed description of exemplary embodiments, which proceeds with reference to the accompanying drawings.
The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate exemplary embodiments, features, and aspects of the present invention and, together with the description, serve to explain the principles of the invention.
FIG. 1 is a block diagram of a process flow of an embodiment of the present invention;
FIG. 2 is a schematic structural view of a wastewater treatment plant according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of the catalytic reactor of FIG. 2;
FIG. 4 is a schematic view of a process of a wastewater treatment apparatus according to an embodiment of the present invention.
Detailed Description
Various exemplary embodiments, features and aspects of the present invention will be described in detail below with reference to the accompanying drawings. In the drawings, like reference numbers can indicate functionally identical or similar elements. While the various aspects of the embodiments are presented in drawings, the drawings are not necessarily drawn to scale unless specifically indicated.
The application provides a effluent treatment plant based on Membrane Bioreactor (MBR) throws (pours into) catalytic oxidation into with ozone multiple spot, and this effluent treatment plant includes: a Membrane Bioreactor (MBR), a suction pump, a membrane effluent lifting pool, a membrane effluent lifting pump, a catalytic reactor and a discharge water pool; when the device is operated, the water treated by the membrane bioreactor is introduced into the membrane effluent lifting tank by the suction pump, then is lifted to the water inlet of the catalytic reactor by the membrane effluent lifting pump, and is treated by O in the catalytic reactor3/H2O2And discharging the treated waste water to a discharge water pool. The catalytic reactor is of a pipeline structure and comprises a hydrogen peroxide feeding port arranged near a water inlet and a plurality of ozone feeding ports, wherein ozone and H are arranged in the catalytic reactor2O2Fully mixing with water, and generating hydroxyl free radicals by ozone under the action of hydrogen peroxide to oxidize and degrade macromolecular nondegradable organic matters in water into micromolecular substances and CO2And water, and the degraded water is discharged through a water outlet. Preferably, the suction pump matched with the membrane module can be directly connected to the inlet of the catalytic reactor under the condition that the membrane module normally operates and is not cleaned, so that water treated by the MBR is not discharged into the membrane water outlet lifting pool and directly enters the catalytic reactor. Thus, the device is provided withThe method saves a precipitation process, has simple and convenient process, produces low suspended matters and turbidity in the effluent, and effectively improves the reaction efficiency of the catalytic oxidation of the ozone.
The operation of the wastewater treatment plant according to the embodiment of the present application will be described with reference to fig. 1, and the process is as follows: effluent treated by the Membrane Bioreactor (MBR) is sucked by negative pressure through a suction pump matched with the membrane component, and is discharged into a membrane effluent lifting pond after being collected by a membrane water collecting manifold. The water is separated from the activated sludge in the membrane bioreactor. The separated water is led to a membrane effluent lifting pond. In one embodiment, the effluent treated by the Membrane Bioreactor (MBR) is directly connected to the catalytic reactor inlet. The membrane component can carry out solid-liquid separation efficiently, the effluent quality is good and stable, and the effluent suspended matter and turbidity are low. When water enters the catalytic reactor, hydrogen peroxide is added near the water inlet of the catalytic reactor, and ozone is added (injected) into the catalytic reactor through a plurality of ozone adding points, so that the water, the ozone and the hydrogen peroxide are fully mixed, and the ozone generates hydroxyl free radicals under the action of the hydrogen peroxide, so that macromolecular refractory organic matters in the wastewater are oxidized and degraded into micromolecular substances and CO2And water, and the effluent can be directly discharged or discharged to a reuse water treatment system.
As shown in fig. 2, which is a schematic structural diagram of a wastewater treatment device based on a combination of a membrane bioreactor and ozone multi-point dosing according to an embodiment of the present application, the wastewater treatment device includes:
a membrane bioreactor 1, a suction pump 2, a membrane effluent lifting pool 3, a membrane effluent lifting pump 4, a catalytic reactor 5 and a discharge water pool 6,
wherein, the membrane bioreactor 1 is provided with a water outlet which is arranged at the upper part of the membrane component and is connected with one end of a membrane water collecting pipe, the other end of the membrane water collecting pipe is connected with a suction pump 2, the water treated by the membrane bioreactor 1 is directly led to the suction pump 2 through the membrane water collecting pipe and is led to a membrane water outlet lifting pool 3 through the suction pump 2,
a membrane effluent lift pump 4 having a first water inlet end connected to the inside of the membrane effluent lift tank 3 through a pipe, a first water outlet end connected to the water inlet of the catalytic reactor 5 through a pipe, the membrane effluent lift pump 4 lifting the water into the catalytic reactor 5 where the water passes through the catalytic reactor 5The water treated by the catalytic oxidation of ozone is led into a discharge water tank 6 through a water outlet of the water treatment tank. In this embodiment, the amount of ozone added can be adjusted to 0-240 mg/L, the retention time of water in the pipeline is 1-10 min, and O is3/H2O2The adding mass ratio of (A) to (B) is 2-3: 1 (in the present embodiment, O)3/H2O2The adding mass ratio of (A) to (B2.83): 1). The ozone adding pressure is 0.09MPa, in order to overcome the head loss in the catalytic reactor, an ozone liquid ring compressor needs to be started while the catalytic reactor is operated for reaction, the exhaust pressure of the ozone is increased to 0.15MPa, and the ozone can be smoothly added into the reactor. Generally, water to be treated is subjected to biochemical treatment in a biochemical tank in advance before flowing into the MBR, the sludge concentration in the biochemical tank is high, the organic matter removal rate is high, and the membrane separation enables macromolecular degradation-resistant components in the sewage to have enough residence time in a membrane bioreactor with a limited volume, so that the culture of special bacteria is facilitated, and the degradation efficiency of the degradation-resistant organic matters is greatly improved. The membrane bioreactor comprises a membrane component made of PVDF hollow fiber membrane material.
As shown in fig. 3, which is a schematic structural diagram of a catalytic reactor, the catalytic reactor 51 is a pipeline type mixing reactor, and includes a water inlet 51, a water outlet 52, a first ozone adding port 53, a second ozone adding port 54, and a third ozone adding port 55, wherein the first ozone adding port 53, the second ozone adding port 54, and the third ozone adding port 55 are respectively connected to an ozone generator (not shown) through pipelines, and H is configured near the water inlet 512O2(also called hydrogen peroxide) feeding port 56, so that water flows to the catalytic reactor through water inlet 51 and simultaneously flows through H2O2The feeding port injects H into the water2O2The front section of the reactor is provided with a mixing zone, a first ozone adding port 53, a second ozone adding port 54 and a third ozone adding port 55 which respectively inject ozone into water, so that ozone and H2O2The ozone generates hydroxyl free radicals under the action of hydrogen peroxide, so that the organic matters which are difficult to degrade and are large molecules in the (waste) water are oxidized and degraded into micromolecular substances and CO2And water, and the degraded water can be directly discharged through the water outlet 52. This embodimentIn the formula, the adding amount of ozone can be adjusted to 0-240 mg/L, preferably, the flow speed of water in the pipeline of the catalytic reactor is 1-3 m/s, and the design ensures that the retention time of water in the reactor is 1-10 min, thereby ensuring the sufficient reaction. O is3/H2O2The adding mass ratio of (A) to (B) is 2-3: 1 (in the present embodiment, O)3/H2O2The adding mass ratio of (A) to (B2.83): 1). When the catalytic reactor operates, because water has a certain flow rate, certain pressure is needed when ozone is injected, and preferably, the ozone adding pressure is 0.09 MPa. In order to overcome the head loss in the catalytic reactor, the ozone liquid ring compressor needs to be started while the catalytic reactor is operated for reaction, and the exhaust pressure of the ozone is 0.1-0.3 MPa, preferably 0.15 MPa. In this embodiment, the first ozone adding port, the second ozone adding port and the third ozone adding port are connected with the ozone liquid ring compressor, the ozone adding unit, the gas-liquid separator and the tube type heat exchanger in a distribution matching manner (not shown). In other embodiments, multiple ozone dosing ports are provided depending on the application.
In one embodiment, the distance L1 between the first ozone dosing port and the second ozone dosing port (i.e., the distance that water flows from the first ozone dosing port to the second ozone dosing port in the pipeline) is equal to or approximately equal to the distance L2 that water flows between the second ozone dosing port and the third ozone dosing port (i.e., the distance that water flows from the second ozone dosing port to the third ozone dosing port in the pipeline). The ratio of the distance L3 (same as L1 and L2) between the third ozone adding port and the water inlet to the distance L (same as L1 and L2) between the water inlet 51 and the water outlet 52 is 0.3-0.7. The design ensures that the ozone and the water have sufficient time for mixing and reaction after mixing after the third ozone adding port injects the ozone. Preferably, the water inlet 51 is the same or substantially the same as the first ozone dosing port 53 in the horizontal position.
In one embodiment, the suction pump 2 associated with the membrane module may be directly connected to the inlet of the catalytic reactor 5 without cleaning during normal operation of the membrane module, and the water treated by the membrane module is not discharged into the membrane effluent lift tank 3.
At one endIn the implementation mode, the coal chemical industry degradation-resistant wastewater enters the membrane bioreactor, the effluent is sucked under negative pressure through a suction pump matched with the membrane component and is discharged into the membrane effluent lifting pond after passing through the membrane water collecting manifold. And lifting the wastewater in the membrane effluent lifting tank to the catalytic reactor. When water enters the catalytic reactor, ozone is added at a plurality of ozone adding points of the reactor, hydrogen peroxide is added at the water inlet end of the reactor, the water, the ozone and the hydrogen peroxide are fully mixed, and the ozone generates hydroxyl radicals under the action of the hydrogen peroxide, so that macromolecular refractory organic matters in the wastewater are oxidized and degraded into micromolecular substances and CO2And water is mixed, and the effluent can be directly discharged. The adding amount of ozone is 100mg/L, the reaction time can be set to 5min, O3/H2O2The adding mass ratio of (A) to (B2.83): 1. when the catalytic reactor reacts, an ozone liquid ring compressor needs to be started, the exhaust pressure of ozone is increased to 0.15MPa, and a water sample is taken to measure COD after the effluent is stable. COD is reduced from 100mg/L to 70mg/L, and the removal rate of COD reaches 30 percent. This embodiment ensures that the COD of the waste water is reduced by controlling the reasonable ozone dosage.
In one embodiment, the coal chemical industry degradation-resistant wastewater enters the membrane bioreactor, and then the effluent is pumped under negative pressure by a suction pump matched with the membrane module, and is discharged into the membrane effluent lifting pond after passing through the membrane water collection manifold. And lifting the wastewater in the membrane effluent lifting tank to the catalytic reactor. When water enters the catalytic reactor, ozone is added at a plurality of ozone adding points of the reactor, hydrogen peroxide is added at the water inlet end of the reactor, the water, the ozone and the hydrogen peroxide are fully mixed, and the ozone generates hydroxyl radicals under the action of the hydrogen peroxide, so that macromolecular refractory organic matters in the wastewater are oxidized and degraded into micromolecular substances and CO2And water is mixed, and the effluent can be directly discharged. The adding amount of ozone is 150mg/L, the reaction time can be set to 5min, O3/H2O2The adding mass ratio of (A) to (B2.83): 1. when the catalytic reactor reacts, an ozone liquid ring compressor needs to be started, the exhaust pressure of ozone is increased to 0.15MPa, and a water sample is taken to measure COD after the effluent is stable. COD is reduced from 100mg/L to 50mg/L, and the removal rate of COD reaches 50%. By controlling reasonable ozone adding amount, the COD of the wastewater can reach 50mg/L, and the wastewater can be discharged up to the standard or directly enter a reuse water treatment system。
The application also provides a wastewater treatment method (also called wastewater treatment process) based on a membrane bioreactor and ozone multipoint adding combination, which comprises the wastewater treatment equipment, and the method comprises the following steps:
s1, water to be treated flows into a membrane bioreactor;
s2, separating the wastewater from the activated sludge in the membrane bioreactor based on the membrane bioreactor wastewater;
s3, lifting the separated water to a catalytic reactor, adding hydrogen peroxide to the water inlet end of the reactor while feeding water into the reactor, adding ozone to a plurality of ozone adding points of the reactor, fully mixing the water, the ozone and the hydrogen peroxide, and generating hydroxyl radicals by the ozone under the action of the hydrogen peroxide so as to oxidize and degrade macromolecular nondegradable organic matters in the water into micromolecular substances and CO2And water.
And S4, discharging the water treated by the reactor to a discharge water pool. In the embodiment, the water (also called as effluent) treated by the membrane bioreactor omits a precipitation process, the process is simple and convenient, the suspended matters and turbidity of the effluent are low, and the reaction efficiency of the catalytic oxidation of ozone is effectively improved. In this embodiment, the membrane module included in the membrane bioreactor is a PVDF hollow fiber membrane. Preferably, the membrane flux of the membrane is 12L/(m)2H). The adding pressure of ozone is 0.09 MPa. Because the wastewater generates resistance to ozone feeding after entering the catalytic reactor, an ozone liquid ring compressor needs to be started preferably, and the exhaust pressure is 0.15 MPa. Ozone (O) in S33) Hydrogen peroxide (H)2O2) The adding mass ratio of (A) to (B2.83): 1, 250mg/L ozone consumption is required for every 100mg/LCOD removal.
The flow speed of water in the catalytic reactor pipeline is 1-3 m/s. The residence time of the water in the reactor is 1-10 min, so that the sufficient reaction is ensured. The reactor is provided with 3 ozone adding points, the adding amount of ozone at each adding amount point is 20mg/L, and the maximum adding amount of ozone is 240 mg/L. Compared with single-point addition, the contact of water, ozone and hydrogen peroxide is insufficient. If hydrogen peroxide is added into the water inlet of the reactor and ozone is added at a single point, the reaction is only carried out at the front section of the reactor, and the catalytic oxidation capability is basically lost at the rear section of the reactor. The application uses 3 point locations, which are generally equally spaced along the length of the pipe, in order to allow more complete contact between ozone and water.
In one embodiment, the S1 further includes that the water to be treated, which is difficult to degrade in the coal chemical industry, flows into the membrane bioreactor after being subjected to biochemical treatment. The biochemical reaction depends on the characteristics of the wastewater, and any biochemical process can be selected according to the characteristics of the wastewater, and the biochemical effluent enters the MBR membrane tank.
In one embodiment, in S3, in the case that the membrane module is normally operated without backwashing, a suction pump matched with the membrane module may be directly connected to the inlet of the catalytic reactor.
In one embodiment, the step S3 further includes pumping the separated water to the membrane effluent lifting pond by the negative pressure of the suction pump.
The above embodiments are only for illustrating the technical concept and features of the present invention, and the purpose of the embodiments is to enable those skilled in the art to understand the contents of the present invention and to implement the present invention, which cannot limit the protection scope of the present invention. All modifications made according to the spirit of the main technical scheme of the present invention shall be covered within the protection scope of the present invention.
Claims (10)
1. A wastewater treatment device based on combination of MBR and ozone multi-point feeding is characterized by comprising a membrane bioreactor, a suction pump, a catalytic reactor and a discharge water tank,
the membrane bioreactor is provided with a water outlet which is arranged at the upper part of the membrane component and is connected with one end of a membrane water collecting pipe, the other end of the membrane water collecting pipe is connected with a suction pump,
the catalytic reactor has the water inlet, and it is connected to the suction pump through the pipeline, and the delivery port, it is connected to the emission pond through the pipeline, and port is thrown to a plurality of ozone, and it is used for to catalytic reactor's intraductal injection ozone, hydrogen peroxide solution throw the port, and it is located near the water inlet, be used for to catalytic reactor's intraductal injection hydrogen peroxide solution, wherein, the water process of membrane bioreactor processing is taken out and is introduced catalytic reactor, and the water after ozone catalytic oxidation handles is discharged to the emission pond through its export in catalytic reactor.
2. The MBR-based and ozone multi-point dosing combined wastewater treatment device of claim 1, wherein the ozone dosage at each ozone dosing port is 20mg/L to 80 mg/L.
3. The MBR and ozone multi-point dosing combination-based wastewater treatment device of claim 1, further comprising a membrane effluent lifting tank, wherein the water treated by the membrane bioreactor is introduced to the membrane effluent lifting tank through a suction pump;
the membrane water outlet lifting pump is provided with a first water inlet end which is connected into the membrane water outlet lifting pool through a pipeline, and a first water outlet end which is connected to a water inlet of the catalytic reactor through a pipeline and is used for lifting water in the membrane water outlet lifting pool to the catalytic reactor.
4. The MBR-based and ozone multi-point dosing combined wastewater treatment device of claim 1, wherein the total ozone dosage of the plurality of ozone dosing ports is 0-240 mg/L.
5. The wastewater treatment device based on MBR and ozone multi-point feeding combination as claimed in claim 1, 2 or 3, wherein the feeding mass ratio of ozone to hydrogen peroxide is 2-3: 1.
6. the MBR and ozone multi-point dosing combination-based wastewater treatment device of claim 5, wherein the dosing amount of the ozone and the hydrogen peroxide is 2.83: 1.
7. the MBR and ozone multi-point dosing combination-based wastewater treatment device as set forth in claim 1, wherein the membrane bioreactor comprises a membrane module made of PVDF hollow fiber membrane material; the adding pressure of the ozone is 0.09 MPa.
8. The wastewater treatment device based on MBR and ozone multipoint adding combination as claimed in claim 1, wherein the catalytic reactor is a pipeline type mixing reactor, and comprises a water inlet, a water outlet, a first ozone adding port, a second ozone adding port and a third ozone adding port, wherein the first ozone adding port, the second ozone adding port and the third ozone adding port are respectively connected to an ozone generator through pipelines, a hydrogen peroxide adding port is configured near the water inlet, water flows to the catalytic reactor through the water inlet during the operation of the catalytic reactor, and the hydrogen peroxide adding port is used for injecting hydrogen peroxide, the first ozone adding port, the second ozone adding port and the third ozone adding port into the water in the pipelines.
9. The MBR-and-ozone multi-point dosing combination-based wastewater treatment plant of claim 8, wherein the distance L1 between the first and second ozone dosing ports is equal to the distance L2 between the second and third ozone dosing ports.
10. The MBR and ozone multi-point dosing combination-based wastewater treatment device of claim 8, wherein the ratio of the distance L3 between the third ozone dosing port and the water inlet to the distance L between the water inlet and the water outlet is 0.3-0.7.
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| CN110526497A (en) * | 2019-08-22 | 2019-12-03 | 麦王环境技术股份有限公司 | A kind of wastewater treatment equipment and method based on MBR in conjunction with ozone multi-point adding |
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| CN110526497A (en) * | 2019-08-22 | 2019-12-03 | 麦王环境技术股份有限公司 | A kind of wastewater treatment equipment and method based on MBR in conjunction with ozone multi-point adding |
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Address after: Floor 4, block a, Oriental fisherman's Wharf, 1088 Yangshupu Road, Yangpu District, Shanghai 200082 Patentee after: Mai Wang Environmental Technology Co.,Ltd. Country or region after: China Address before: Floor 4, block a, Oriental fisherman's Wharf, 1088 Yangshupu Road, Yangpu District, Shanghai 200082 Patentee before: MCWONG ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Country or region before: China |
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